US4271008A - Production of ethylene - Google Patents
Production of ethylene Download PDFInfo
- Publication number
- US4271008A US4271008A US06/098,609 US9860979A US4271008A US 4271008 A US4271008 A US 4271008A US 9860979 A US9860979 A US 9860979A US 4271008 A US4271008 A US 4271008A
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- US
- United States
- Prior art keywords
- gas mixture
- sub
- aluminum
- reaction
- heated
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/002—Avoiding undesirable reactions or side-effects, e.g. avoiding explosions, or improving the yield by suppressing side-reactions
- B01J19/0026—Avoiding carbon deposits
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/04—Thermal processes
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S585/00—Chemistry of hydrocarbon compounds
- Y10S585/949—Miscellaneous considerations
- Y10S585/95—Prevention or removal of corrosion or solid deposits
Definitions
- This invention relates to a process for making ethylene by subjecting a gas mixture containing hydrocarbons, hydrogen, carbon monoxide, carbon dioxide and steam to a hydropyrolysis reaction.
- a process for making ethane and/or ethylene has been described, wherein a reaction mixture consisting of hydrocarbons, carbon monoxide, carbon dioxide, water and hydrogen (the mixture being obtained by reacting hydrogen with carbon monoxide in a molar ratio of 1:1 to 5:1 in contact with a Fischer-Tropsch catalyst containing iron, cobalt, nickel or ruthenium) is pyrolyzed inside a hydropyrolyzing zone at a temperature of 600° to 900° C., under a pressure of at least 5 bars and over a period of 0.1 to 60 seconds, and the resulting gas mixture issuing from the hydropyrolyzing zone is treated so as to separate C 2 -hydrocarbons therefrom.
- a reaction mixture consisting of hydrocarbons, carbon monoxide, carbon dioxide, water and hydrogen (the mixture being obtained by reacting hydrogen with carbon monoxide in a molar ratio of 1:1 to 5:1 in contact with a Fischer-Tropsch catalyst containing iron, cobalt, nickel or ruthenium
- a quartz tube should conveniently be used for subjecting a gas mixture containing hydrocarbons, hydrogen, carbon monoxide, carbon dioxide and steam to hydropyrolysis therein.
- a quartz tube it has been possible to effect the reaction over a period of 250 hours substantially without undesirable disturbing deposition of carbon black. If carried out in a tube made up, e.g. of iron, temperature-resistant steels or nickel, the reaction just described is normally accompanied by undesirable formation of carbon black or decomposition of hydrocarbons.
- the present invention relates more particularly to a process for the commercial production of ethylene by subjecting a gas mixture containing hydrocarbons, hydrogen, carbon monoxide, carbon dioxide and water to a pyrolysis reaction permitting the formation of carbon black (which may ultimately result in the tubular reactors becoming clogged therewith) and decomposition of hydrocarbons to be substantially avoided.
- the invention provides for the gas mixture to be heated to temperatures higher than 800° C. inside a reaction zone having metal walls containing aluminum and/or copper in at least their surface portions facing and coming into contact with the gas mixture.
- Materials which can be used for making the walls of the reaction zone comprise chrome and chrome-nickel steels which additionally contain aluminum, e.g. ALUCHROM (this is a registered Trade Mark; construction materials nos. 1.4765 and 1,4767 according to DIN-specification (DIN stands for German Industrial Standard) 17 470, July 1963); ARMCO 18 SR (this is a registered Trade Mark) or KANTHAL (this is a registered Trade Mark).
- ALUCHROM this is a registered Trade Mark
- ARMCO 18 SR this is a registered Trade Mark
- KANTHAL this is a registered Trade Mark
- One method of applying aluminum to the inside walls of a reaction zone comprises filling the zone with a mixture of pulverulent or granular aluminum and a porous carrier which does not react with aluminum, e.g. aluminum oxide, and annealing the mixture at 700° to 1000° C. under scavenging treatment with a mixture of nitrogen and aluminum chloride in vapor form. During that treatment which is effected over a period of 2 to 5 hours, it is possible for sufficient aluminum to diffuse into, and catalytically inactivate, the metal walls of the reaction zone.
- Another method of applying aluminum to the inside walls of the reactor comprises filling the reactor with an aluminum melt of 700° to 900° C. and leaving the walls in contact therewith over 2 to 20 hours.
- Another method of reliably reducing the catalytic activity of metal walls comprises using the aluminum in further admixture with copper powder, copper granules or a copper melt, and contacting the metal walls therewith.
- Still another method of reducing the catalytic activity of reactor inside walls comprises using the gas mixture in further admixture with one or more sulfur-containing compounds, e.g. H 2 S, CS 2 and COS, and contacting the metal walls therewith.
- one or more sulfur-containing compounds e.g. H 2 S, CS 2 and COS
- the gas mixture used in each particular case was left uncooled and, after pressure release to 1 bar, it was introduced into a hydropyrolysis reactor of which the tubular structures which were heated over a length of 20 cm had an internal diameter of 10 mm.
- the various materials used for making the tubular structures are indicated in the following Table 2.
- the residence time of the gas mixture in the tubular structures was about 0.25 second, under the experimental conditions selected (1 bar; 890° C.). In Examples 13 to 22 listed in Table 2, the change in volume varied by about -10%.
Abstract
The invention relates to a process for making ethylene by subjecting a gas mixture containing hydrocarbons, hydrogen, carbon monoxide, carbon dioxide and steam to a hydropyrolysis reaction. More particularly, the gas mixture is heated to temperatures higher than 800 DEG C. inside a reaction zone having metal walls. The walls contain aluminum and/or copper in at least their surface portions.
Description
This invention relates to a process for making ethylene by subjecting a gas mixture containing hydrocarbons, hydrogen, carbon monoxide, carbon dioxide and steam to a hydropyrolysis reaction.
A process for making ethane and/or ethylene has been described, wherein a reaction mixture consisting of hydrocarbons, carbon monoxide, carbon dioxide, water and hydrogen (the mixture being obtained by reacting hydrogen with carbon monoxide in a molar ratio of 1:1 to 5:1 in contact with a Fischer-Tropsch catalyst containing iron, cobalt, nickel or ruthenium) is pyrolyzed inside a hydropyrolyzing zone at a temperature of 600° to 900° C., under a pressure of at least 5 bars and over a period of 0.1 to 60 seconds, and the resulting gas mixture issuing from the hydropyrolyzing zone is treated so as to separate C2 -hydrocarbons therefrom. For effecting the hydropyrolysis reaction just described, use can be made of a reactor which has a heat-resistant steel cylinder placed therein, which faces and comes into contact with the reaction mixture. As to those mixtures which are obtained by the catalytic reduction of carbon monoxide with hydrogen by a process, such as described in British Patent Specification Nos. 1,515,604, 1,554,082 and 1,548,527, respectively, it is only possible for them to be subjected to hydropyrolysis provided that equilibrium establishment for the following reactions
H.sub.2 +CO.sub.2 →H.sub.2 O+CO
--CH.sub.2 --+H.sub.2 O→CO+2H.sub.2
--CH.sub.2 --+2CO.sub.2 →3CO+H.sub.2 O
is avoided at the necessary temperature range of about 800° to 950° C. and also provided that neither the hydrocarbons nor carbon monoxide produce carbon black in quantities which are liable to adversely affect operation.
Unless catalytically promoted by contact of the reaction mixture with the wall of the pyrolysis reactor, the above reactions occur so reluctantly that they cannot reasonably be said to impair the yield of olefins formed by hydropyrolysis during the necessary short contact time of 0.02 to 2 seconds.
It has also been described that a quartz tube should conveniently be used for subjecting a gas mixture containing hydrocarbons, hydrogen, carbon monoxide, carbon dioxide and steam to hydropyrolysis therein. In a quartz tube, it has been possible to effect the reaction over a period of 250 hours substantially without undesirable disturbing deposition of carbon black. If carried out in a tube made up, e.g. of iron, temperature-resistant steels or nickel, the reaction just described is normally accompanied by undesirable formation of carbon black or decomposition of hydrocarbons.
The present invention relates more particularly to a process for the commercial production of ethylene by subjecting a gas mixture containing hydrocarbons, hydrogen, carbon monoxide, carbon dioxide and water to a pyrolysis reaction permitting the formation of carbon black (which may ultimately result in the tubular reactors becoming clogged therewith) and decomposition of hydrocarbons to be substantially avoided.
To this end, the invention provides for the gas mixture to be heated to temperatures higher than 800° C. inside a reaction zone having metal walls containing aluminum and/or copper in at least their surface portions facing and coming into contact with the gas mixture.
Preferred features of the present process provide:
(a) for the gas mixture to be heated to temperatures higher than 900° C.;
(b) for the gas mixture to be heated to temperatures up to 1000° C.;
(c) for the heated gas mixture to be maintained under a pressure of less than 5 bars;
(d) for the heated gas mixture to be maintained under a pressure within the range 1.5 to 4 bars;
(e) for the metal walls of the reaction zone to be made up of steel containing aluminum and/or copper;
(f) for the metal walls of the reaction zone to have aluminum and/or copper applied thereto;
(g) for the aluminum and/or copper to be applied to the metal walls via the gas phase with the use of one or more halogen compounds as transporting agent;
(h) for the aluminum and/or copper to be applied to the metal walls by contacting the latter with an aluminum and/or copper melt; and
(i) for the gas mixture to be used in further admixture with one or more gaseous sulfur compounds.
Materials which can be used for making the walls of the reaction zone comprise chrome and chrome-nickel steels which additionally contain aluminum, e.g. ALUCHROM (this is a registered Trade Mark; construction materials nos. 1.4765 and 1,4767 according to DIN-specification (DIN stands for German Industrial Standard) 17 470, July 1963); ARMCO 18 SR (this is a registered Trade Mark) or KANTHAL (this is a registered Trade Mark). In those cases in which steel substantially free from aluminum is used for making the walls of the reaction zone, it is necessary for aluminum to be applied to that side of the walls which faces and comes into contact with the gas mixture. Even aluminum-containing steel should have additional aluminum applied thereto as this permits the catalytic activity of the reactor walls to be further reduced.
One method of applying aluminum to the inside walls of a reaction zone comprises filling the zone with a mixture of pulverulent or granular aluminum and a porous carrier which does not react with aluminum, e.g. aluminum oxide, and annealing the mixture at 700° to 1000° C. under scavenging treatment with a mixture of nitrogen and aluminum chloride in vapor form. During that treatment which is effected over a period of 2 to 5 hours, it is possible for sufficient aluminum to diffuse into, and catalytically inactivate, the metal walls of the reaction zone.
Another method of applying aluminum to the inside walls of the reactor comprises filling the reactor with an aluminum melt of 700° to 900° C. and leaving the walls in contact therewith over 2 to 20 hours. Another method of reliably reducing the catalytic activity of metal walls comprises using the aluminum in further admixture with copper powder, copper granules or a copper melt, and contacting the metal walls therewith.
Still another method of reducing the catalytic activity of reactor inside walls comprises using the gas mixture in further admixture with one or more sulfur-containing compounds, e.g. H2 S, CS2 and COS, and contacting the metal walls therewith.
In all of the following Examples, use was made of a gas mixture which was obtained by contacting a mixture of carbon monoxide and hydrogen which were used in a ratio by volume of 1:1, at 290° C. and under 16 bars with a carrier-supported catalyst containing iron, copper and potassium. The composition typical of the gas mixture is indicated in the following Table 1, left hand column.
The gas mixture used in each particular case was left uncooled and, after pressure release to 1 bar, it was introduced into a hydropyrolysis reactor of which the tubular structures which were heated over a length of 20 cm had an internal diameter of 10 mm. The various materials used for making the tubular structures are indicated in the following Table 2. The residence time of the gas mixture in the tubular structures was about 0.25 second, under the experimental conditions selected (1 bar; 890° C.). In Examples 13 to 22 listed in Table 2, the change in volume varied by about -10%.
As would appear to result from Table 2, comparative Examples 1 to 12, the tubular structures made from the materials specified were found to promote the formation of carbon black (which results in the tubular structures becoming ultimately clogged therewith) and/or to effect an increase in the CO-content and/or to produce reaction gas of low ethylene concentration.
This is in clear contrast with the results obtained with tubular structures made from materials in accordance with this invention (Examples 13 to 22). Reaction gas of high ethylene concentration was obtained. Even after prolonged operation, carbon black could not be found to have been formed. Nor could the CO-concentration be found to have been significantly increased, based on the CO-concentration of the feed gas mixture.
The analytical data typical of a gas obtained by the present hydropyrolysis process is indicated in Table 1, right hand portion.
In Table 2, the sign "a→b" indicates that the concentration in the hydropyrolysis gas changed from (a) to (b) volume % during the experiment.
TABLE 1 ______________________________________ Hydropyrolysis gas Gas mixture C - % Com- Com- Yield based on posi- Selec- posi- %, based sum of tion tivity tion on CO hydro- vol. % % vol. % reacted carbons ______________________________________ H.sub.2 O 2.85 2.79 O.sub.2 0.59 0.48 N.sub.2 0.24 0.24 H.sub.2 26.42 29.62 CO 14.33 13.48 CO.sub.2 34.32 46.51 31.34 47.12 -- CH.sub.4 12.80 17.35 12.89 19.48 36.84 C.sub.2 H.sub.2 <0.01 0.37 1.12 2.11 C.sub.2 H.sub.4 0.59 9.27 6.84 20.67 39.10 C.sub.2 H.sub.6 2.32 0.53 1.60 3.03 C.sub.3 2.41 9.80 0.59 2.67 5.06 C.sub.4 2.35 12.74 0.12 0.37 1.37 C.sub.5 0.54 3.66 0.26 C.sub.6 0.15 1.22 0.09 C.sub.7 0.04 0.38 0.25 6.76 12.78 C.sub.8 <0.02 <0.22 0.07 C.sub.8+ <0.02 ˜0.22 ˜0.04 ______________________________________
TABLE 2 __________________________________________________________________________ Operation content Material used for making period CO-increase vol. % tubular structure (h) vol. % CH.sub.4 C.sub.2 H.sub.4 observations __________________________________________________________________________ (Comparative Examples) 1 Iron 14 18 → 0 17 4.2 clogged by 2 Iron, S-treated 24 4 → 0 16 → 9 5.9 → 0.4 carbon black 3 Iron, P-treated 4 5 → 20 13 6 → 0.7 4 Iron, treated with 6 10 15 6 → 3.5 silicic acid ester 5 Iron, treated with 18 16 → 2 11 → 8 2.8 → 0.4 silicic acid ester; annealed for 4 h 6 Iron, treated with 3 5 → 15 12 → 17 5.5 → 18 silicic acid ester; annealed for 4 h sulfided gas mixture 7 Iron, gold-plated 22 30 9 1.5 with H(AuCl.sub.4) 8 Steel; material no. 19 3 12.8 5.9 carbon black 1.4016 formation (CEKAS; Reg. Trade -ark) 9 Steel; material no. 21 1 15.2 6.0 carbon black 1.4016 (CEKAS; Reg. Trade Mark); formation sulfided gas mixture 10 Steel; material no. 22 16 10.6 1.1 1.4841 11 Steel; material no. 12 18 12 4.2 → 2.0 1.4541 -12 Pure nickel, polished 16 11 22.4 1.0 carbon black formation (Examples in accordance with invention) 13 ALUCHROM O 250 0.5 16 6.2 spontaneous 14 ALUCHROM O; sulfided 250 0 14.8 5.7 ethylene drop gas mixture after 89 h 15 ALUCHROM W 92 0 14.6 7.1 16 KANTHAL DSD 250 0 12.2 5.25 17 INCONEL 601; 250 1 16 6.9 Al-plated 18 ARMCO 18 SR 250 2.6 16.8 6.6 19 ARMCO 18 SR; Al-plated 250 1.5 16.8 7.2 20 Steel; material no. 250 0 15.6 6.2 1.4571 plated with Al and Cu 21 Steel; material no. 250 0 16.4 6.7 1.4571; Al-plated 22 Steel; material no. 250 -3.3 14.3 5.7 1.4571; Cu-plated __________________________________________________________________________
Claims (5)
1. A process for making ethylene by subjecting a gas mixture containing hydrocarbons, hydrogen, carbon monoxide, carbon dioxide and steam to a hydropyrolysis reaction, which comprises heating the gas mixture to temperatures higher than 800° C. and maintaining the heated gas mixture under a pressure of less than 5 bars inside a reaction zone having metal walls made up of steel containing copper.
2. A process for making ethylene by subjecting a gas mixture containing hydrocarbons, hydrogen, carbon monoxide, carbon dioxide and steam to a hydropyrolysis reaction, which comprises heating the gas mixture to temperatures higher than 800° C. and maintaining the heated gas mixture under a pressure of less than 5 bars inside a reaction zone having metal walls coated with an overlayer of at least one metal selected from copper and aluminum, said overlayer being applied to the metal walls via the gas phase with the use of at least one halogen compound as a transporting agent.
3. The process as claimed in claim 1 or 2, wherein the gas mixture is heated to temperatures of 900°-1000° C.
4. The process as claimed in claim 1 or 2, wherein the heated gas mixture is maintained under a pressure of 1.5-4 bars.
5. The process as claimed in claim 1 or 2, wherein the gas mixture is used in further admixture with at least one gaseous sulfur compound.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE2852314 | 1978-12-04 | ||
DE19782852314 DE2852314A1 (en) | 1978-12-04 | 1978-12-04 | METHOD FOR PRODUCING ETHYLENE |
Publications (1)
Publication Number | Publication Date |
---|---|
US4271008A true US4271008A (en) | 1981-06-02 |
Family
ID=6056233
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US06/098,609 Expired - Lifetime US4271008A (en) | 1978-12-04 | 1979-11-29 | Production of ethylene |
Country Status (6)
Country | Link |
---|---|
US (1) | US4271008A (en) |
EP (1) | EP0011874B1 (en) |
JP (1) | JPS5579328A (en) |
CA (1) | CA1111075A (en) |
DE (2) | DE2852314A1 (en) |
ZA (1) | ZA796546B (en) |
Cited By (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4527003A (en) * | 1983-03-03 | 1985-07-02 | Mitsubishi Jukogyo Kabushiki Kaisha | Thermal cracking process for producing olefins from hydrocarbons |
US4545893A (en) * | 1984-07-20 | 1985-10-08 | Phillips Petroleum Company | Antifoulants for thermal cracking processes |
US4575413A (en) * | 1984-07-06 | 1986-03-11 | Exxon Research & Engineering Co. | Aluminum stearate and/or acetate antifoulants for refinery operations |
US4599478A (en) * | 1983-02-18 | 1986-07-08 | Mitsubishi Jukogyo Kabushiki Kaisha | Thermal cracking method for producing olefines from hydrocarbons |
US4599480A (en) * | 1985-07-12 | 1986-07-08 | Shell Oil Company | Sequential cracking of hydrocarbons |
US4725349A (en) * | 1984-04-13 | 1988-02-16 | Mitsubishi Jukogyo Kabushiki Kaisha | Process for the selective production of petrochemical products |
US5575902A (en) * | 1994-01-04 | 1996-11-19 | Chevron Chemical Company | Cracking processes |
US5593571A (en) * | 1993-01-04 | 1997-01-14 | Chevron Chemical Company | Treating oxidized steels in low-sulfur reforming processes |
US5674376A (en) * | 1991-03-08 | 1997-10-07 | Chevron Chemical Company | Low sufur reforming process |
US5723707A (en) * | 1993-01-04 | 1998-03-03 | Chevron Chemical Company | Dehydrogenation processes, equipment and catalyst loads therefor |
US5849969A (en) * | 1993-01-04 | 1998-12-15 | Chevron Chemical Company | Hydrodealkylation processes |
US6258256B1 (en) | 1994-01-04 | 2001-07-10 | Chevron Phillips Chemical Company Lp | Cracking processes |
US6274113B1 (en) | 1994-01-04 | 2001-08-14 | Chevron Phillips Chemical Company Lp | Increasing production in hydrocarbon conversion processes |
US6419986B1 (en) | 1997-01-10 | 2002-07-16 | Chevron Phillips Chemical Company Ip | Method for removing reactive metal from a reactor system |
US20030135077A1 (en) * | 2002-01-14 | 2003-07-17 | O'rear Dennis J. | Olefin production from low sulfur hydrocarbon fractions |
USRE38532E1 (en) | 1993-01-04 | 2004-06-08 | Chevron Phillips Chemical Company Lp | Hydrodealkylation processes |
WO2010059224A1 (en) * | 2008-11-19 | 2010-05-27 | Global Energies, Llc | Low co2 emissions system |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2114599B (en) * | 1982-01-21 | 1986-07-16 | Jgc Corp | Apparatus for treating hydrocarbons or carbon monoxide-containing fluid high temperatures substantially without carbon deposition |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB364043A (en) * | 1930-07-17 | 1931-12-17 | British & Dominions Feralloy L | Improvements in and relating to the catalytic treatment of hydrocarbons at high temperatures |
US2621216A (en) * | 1950-08-17 | 1952-12-09 | Shell Dev | Production of ethylene |
US3827967A (en) * | 1973-08-30 | 1974-08-06 | Shell Oil Co | Thermal cracking of hydrocarbons |
Family Cites Families (10)
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BE400959A (en) * | 1933-02-24 | |||
AT153171B (en) * | 1935-07-24 | 1938-04-25 | Matthaeus Braun | Process for copper-plating the inside of seamless or welded steel pipes. |
US2343866A (en) * | 1938-10-07 | 1944-03-14 | Wulff Process Company | Process for the pyrolysis of hydrocarbons |
AT189008B (en) * | 1954-05-31 | 1957-02-25 | Erich Dr Ing Fitzer | Process for the production of aluminum coatings and application of this process for the production of powdery aluminum alloys |
US3778488A (en) * | 1970-01-26 | 1973-12-11 | Petro Tex Chem Corp | Iron alloy catalyzed oxidative dehydrogenation |
US3798283A (en) * | 1972-03-08 | 1974-03-19 | Atlantic Richfield Co | Non-catalytic oxidative dehydrogenation process |
JPS552472B2 (en) * | 1974-02-25 | 1980-01-21 | ||
SU701529A3 (en) * | 1975-04-03 | 1979-11-30 | Контитентал Ойл Компани (Фирма) | Method of producing ethane ano/or ethylene |
DE2527316A1 (en) * | 1975-06-19 | 1976-12-30 | Continental Oil Co | Ethane-ethylene prodn. from carbon monoxide and hydrogen - with hydropyrolysis of catalytic reaction zone effluent |
DE2528554A1 (en) * | 1975-06-26 | 1977-01-13 | Continental Oil Co | Ethylene and methane prodn. - by combined hydropyrolysis and cracking of higher hydrocarbons |
-
1978
- 1978-12-04 DE DE19782852314 patent/DE2852314A1/en not_active Withdrawn
-
1979
- 1979-11-21 CA CA340,324A patent/CA1111075A/en not_active Expired
- 1979-11-29 US US06/098,609 patent/US4271008A/en not_active Expired - Lifetime
- 1979-12-01 DE DE7979104817T patent/DE2962847D1/en not_active Expired
- 1979-12-01 EP EP79104817A patent/EP0011874B1/en not_active Expired
- 1979-12-03 JP JP15569979A patent/JPS5579328A/en active Pending
- 1979-12-03 ZA ZA00796546A patent/ZA796546B/en unknown
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB364043A (en) * | 1930-07-17 | 1931-12-17 | British & Dominions Feralloy L | Improvements in and relating to the catalytic treatment of hydrocarbons at high temperatures |
US2621216A (en) * | 1950-08-17 | 1952-12-09 | Shell Dev | Production of ethylene |
US3827967A (en) * | 1973-08-30 | 1974-08-06 | Shell Oil Co | Thermal cracking of hydrocarbons |
Cited By (28)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4599478A (en) * | 1983-02-18 | 1986-07-08 | Mitsubishi Jukogyo Kabushiki Kaisha | Thermal cracking method for producing olefines from hydrocarbons |
US4599479A (en) * | 1983-03-03 | 1986-07-08 | Mitsubishi Jukogyo Kabushiki Kaisha | Thermal cracking process for producing olefins from hydrocarbons |
US4527003A (en) * | 1983-03-03 | 1985-07-02 | Mitsubishi Jukogyo Kabushiki Kaisha | Thermal cracking process for producing olefins from hydrocarbons |
US4725349A (en) * | 1984-04-13 | 1988-02-16 | Mitsubishi Jukogyo Kabushiki Kaisha | Process for the selective production of petrochemical products |
US4575413A (en) * | 1984-07-06 | 1986-03-11 | Exxon Research & Engineering Co. | Aluminum stearate and/or acetate antifoulants for refinery operations |
US4545893A (en) * | 1984-07-20 | 1985-10-08 | Phillips Petroleum Company | Antifoulants for thermal cracking processes |
US4599480A (en) * | 1985-07-12 | 1986-07-08 | Shell Oil Company | Sequential cracking of hydrocarbons |
US5863418A (en) * | 1991-03-08 | 1999-01-26 | Chevron Chemical Company | Low-sulfur reforming process |
US6548030B2 (en) | 1991-03-08 | 2003-04-15 | Chevron Phillips Chemical Company Lp | Apparatus for hydrocarbon processing |
US5674376A (en) * | 1991-03-08 | 1997-10-07 | Chevron Chemical Company | Low sufur reforming process |
US5676821A (en) * | 1991-03-08 | 1997-10-14 | Chevron Chemical Company | Method for increasing carburization resistance |
US5593571A (en) * | 1993-01-04 | 1997-01-14 | Chevron Chemical Company | Treating oxidized steels in low-sulfur reforming processes |
US5849969A (en) * | 1993-01-04 | 1998-12-15 | Chevron Chemical Company | Hydrodealkylation processes |
US5723707A (en) * | 1993-01-04 | 1998-03-03 | Chevron Chemical Company | Dehydrogenation processes, equipment and catalyst loads therefor |
US5866743A (en) * | 1993-01-04 | 1999-02-02 | Chevron Chemical Company | Hydrodealkylation processes |
USRE38532E1 (en) | 1993-01-04 | 2004-06-08 | Chevron Phillips Chemical Company Lp | Hydrodealkylation processes |
US5575902A (en) * | 1994-01-04 | 1996-11-19 | Chevron Chemical Company | Cracking processes |
US6274113B1 (en) | 1994-01-04 | 2001-08-14 | Chevron Phillips Chemical Company Lp | Increasing production in hydrocarbon conversion processes |
US6602483B2 (en) | 1994-01-04 | 2003-08-05 | Chevron Phillips Chemical Company Lp | Increasing production in hydrocarbon conversion processes |
US6258256B1 (en) | 1994-01-04 | 2001-07-10 | Chevron Phillips Chemical Company Lp | Cracking processes |
US6419986B1 (en) | 1997-01-10 | 2002-07-16 | Chevron Phillips Chemical Company Ip | Method for removing reactive metal from a reactor system |
US6551660B2 (en) | 1997-01-10 | 2003-04-22 | Chevron Phillips Chemical Company Lp | Method for removing reactive metal from a reactor system |
US20030135077A1 (en) * | 2002-01-14 | 2003-07-17 | O'rear Dennis J. | Olefin production from low sulfur hydrocarbon fractions |
WO2003059851A1 (en) * | 2002-01-14 | 2003-07-24 | Chevron U.S.A. Inc. | Olefin production from low sulfur hydrocarbon fractions |
US6784329B2 (en) | 2002-01-14 | 2004-08-31 | Chevron U.S.A. Inc. | Olefin production from low sulfur hydrocarbon fractions |
US20050004411A1 (en) * | 2002-01-14 | 2005-01-06 | Chevron U.S.A. Inc. | Olefin production from low sulfur hydrocarbon fractions |
US6979755B2 (en) | 2002-01-14 | 2005-12-27 | Chevron U.S.A. Inc. | Olefin production from low sulfur hydrocarbon fractions |
WO2010059224A1 (en) * | 2008-11-19 | 2010-05-27 | Global Energies, Llc | Low co2 emissions system |
Also Published As
Publication number | Publication date |
---|---|
EP0011874A1 (en) | 1980-06-11 |
JPS5579328A (en) | 1980-06-14 |
CA1111075A (en) | 1981-10-20 |
DE2852314A1 (en) | 1980-06-26 |
ZA796546B (en) | 1980-11-26 |
DE2962847D1 (en) | 1982-07-01 |
EP0011874B1 (en) | 1982-05-12 |
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